KR20180028772A - Pyrolysis apparatus and pyrolysis method for bitumen - Google Patents

Abstract

Disclosed are an apparatus and a method for pyrolyzing a bitumen raw material. According to an embodiment of the present invention, the apparatus for pyrolyzing a bitumen raw material comprises: a storage tank for storing a bitumen raw material; a first pyrolysis reactor for receiving the bitumen raw material from the storage tank, and pyrolyzing the bitumen raw material to generate a first pyrolysis gas and a first inorganic by-product; a first gas-liquid separator for separating the first pyrolysis gas into a first gas product and a first liquid product; a second pyrolysis reactor installed at a lower end of the first pyrolysis reactor, and pyrolyzing the bitumen raw material pyrolyzed in the first pyrolysis reactor again to generate a second pyrolysis gas and a second inorganic by-product; a second gas-liquid separator for separating the second pyrolysis gas into a second gas product and a second liquid product; a first collection tank for collecting the first liquid product; a second collection tank for collecting the second liquid product; and a control unit for controlling the first pyrolysis reactor, the first gas-liquid separator, the second pyrolysis reactor, and the second gas-liquid separator.

Description

[0001] DESCRIPTION [0002] PYROLYSIS APPARATUS AND PYROLYSIS METHOD FOR BITUMEN [

TECHNICAL FIELD The present invention relates to a pyrolysis apparatus and a pyrolysis method for a bituminous raw material.

Recently, there has been a growing debate on the production peak or depletion of petroleum resources, and there is growing interest in the development of non-conventional oil such as bitumen as an alternative to conventional oil.

Although the share of these non-traditional petroleum in the world oil supply market is still small, the US Energy Information Administration (EIA) estimates that by 2035, non-traditional petroleum production will continue to grow in the current Saudi Arabia (797 million bbl / d in April 2010) 90 per cent. In the past 15 years, non-traditional petroleum contributed 7.7% to world oil production, but it is expected to increase to about 21% over the next 15 years.

On the other hand, in terms of profitability of non-traditional petroleum, Venezuela's ultra-heavy oil, Canadian oil sands in terms of supply stability, and the bituminous minerals in Indonesia in terms of availability are regarded as promising petroleum.

Among them, bituminous minerals, which are a kind of bituminous raw material, are buried about 5 billion tons in Indonesia's Buton Island. The recoverable oil content is about 50% or more according to pyrolysis temperature.

The bituminous-containing minerals also contain about 19% of heavy oil (middle oil) having a boiling point of about 950 ° C and a boiling point of about 350 ° C to about 550 ° C, It contains about 32% of heavy oil with a boiling point of about 550 ℃ or more.

As such, the bituminous minerals contain multicomponent oils having different non-viscous properties. Therefore, when the bituminous minerals are recycled into power generation and refinery oil and other by-products, the ripple effect is expected to be large.

However, the bituminous raw materials such as bituminous minerals are still in the early stage of development technology compared to other non - traditional petroleum, and research for utilizing the bituminous raw materials is urgent.

Korean Patent Publication No. 10-2006-0083474 (published on July 21, 2006)

Embodiments of the present invention provide a pyrolysis apparatus and a pyrolysis method of a bituminous raw material capable of continuously recovering oils having different boiling points contained in a raw material for biting.

According to an aspect of the present invention, there is provided a pyrolysis reactor comprising: a storage tank for storing a raw material for biting; a first pyrolysis reactor for receiving the raw raw material from the storage tank and pyrolyzing the raw raw material to produce a first pyrolysis gas and a first inorganic by- 1 a first gas-liquid separator for separating pyrolysis gas into a first gaseous product and a first liquid product; a second gas-liquid separator installed at a lower end of the first pyrolysis reactor, for pyrolyzing the bituminous raw material pyrolyzed in the first pyrolysis reactor, A second gas-liquid separator for separating the second pyrolysis gas into a second gas product and a second liquid product, and a first collecting tank for collecting the first liquid product, A second collecting tank for collecting the second liquid product, and a second collecting tank for collecting the second liquid product, and a second collecting tank for collecting the second liquid product and the first pyrolysis reactor, A thermal decomposition apparatus of the bituminous material comprising a control unit for controlling the Rigi can be provided.

The first gas-liquid separator includes a first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator, and a second pyrolysis gas control unit for controlling a flow rate of the second pyrolysis gas flowing into the second gas- And the control unit may control the opening amount of the first pyrolysis gas control valve and the opening amount of the second pyrolysis gas control valve.

The control unit may control the first pyrolysis reactor to be heated to a first temperature when the bituminous raw material is input to the first pyrolysis reactor.

Also, the controller may control the pyrolysis of the bituminous raw material while the first pyrolytic reactor is gradually heated from the first temperature to the second temperature.

In addition, the controller may control the second pyrolysis reactor to raise the temperature to a third temperature higher than the second temperature.

Also, the controller may control the second pyrolytic reactor to gradually pyrolyze the bituminous raw material while being gradually heated from the third temperature to the fourth temperature.

Also, the controller may control the first pyrolytic reactor to be supplied with the bituminous raw material after the temperature of the first pyrolytic reactor is raised to the first temperature.

In addition, the controller may control the pyrolysis of the bituminous raw material while the first thermal cracking reactor is maintained at the first temperature.

In addition, the controller may control the second pyrolysis reactor to raise the temperature to a second temperature higher than the first temperature.

In addition, the controller may control the pyrolysis of the bituminous raw material while the second thermal cracking reactor is maintained at the second temperature.

A first screw feeder provided between the storage tank and the first pyrolysis reactor and feeding the bituminous raw material stored in the storage tank to the first pyrolysis reactor and a second screw feeder provided between the first pyrolysis reactor and the second pyrolysis reactor And a second screw feeder for transferring the bituminous raw material pyrolyzed in the first pyrolysis reactor to the second pyrolysis reactor.

The heating jacket may further include a heating jacket installed on the outer surface of the storage tank for lowering the viscosity of the bituminous raw material by applying heat to the bituminous raw material stored in the storage tank.

The apparatus may further include a combustion unit that receives and combusts at least one of the first gas product and the second gas product, and the combustion unit may be controlled by the control unit.

The first gas-liquid separator includes a first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator, and a second pyrolysis gas control unit for controlling a flow rate of the second pyrolysis gas flowing into the second gas- And may further include a valve.

The apparatus may further include a first gaseous product control valve for controlling a flow rate of the first gaseous product introduced into the combustion unit and a second gaseous product control valve for controlling a flow rate of the second gaseous product introduced into the combustion unit have.

The control unit may control the amount of opening of the first pyrolysis gas control valve, the amount of opening of the second pyrolysis gas control valve, the amount of opening of the first gas product control valve, and the opening amount of the second gas product control valve, Can be controlled.

The combustion unit may include a combustor that receives and combusts at least one of the first gas product and the second gas product.

The combustion unit may further include a heater provided below the combustor for heating at least one of the first gaseous product and the second gaseous product.

The combustion unit may further include an air supplier connected to the combustor and supplying combustion air to the combustor.

Also, in the combustor, at least one of the first gaseous product and the second gaseous product is burned and exhaust gas is generated, and the exhaust gas is supplied to the combustor connected to the first pyrolysis reactor or the second pyrolysis reactor And the waste heat of the exhaust gas may be used as a heat source for thermal decomposition of the bituminous raw material.

The apparatus may further include a heat exchanger that receives one of the first inorganic byproduct and the second inorganic byproduct and the first and second gaseous products and exchanges heat with each other, Lt; / RTI >

The first gas-liquid separator includes a first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator, and a second pyrolysis gas control unit for controlling a flow rate of the second pyrolysis gas flowing into the second gas- And may further include a valve.

The apparatus may further include a first gaseous product control valve for controlling a flow rate of the first gaseous product introduced into the heat exchanger and a second gaseous product control valve for controlling a flow rate of the second gaseous product introduced into the heat exchanger have.

The control unit may control the amount of opening of the first pyrolysis gas control valve, the amount of opening of the second pyrolysis gas control valve, the amount of opening of the first gas product control valve, and the opening amount of the second gas product control valve, Can be controlled.

According to another aspect of the present invention, there is provided a process for producing a pyrolysis product, comprising the steps of: pyrolyzing a bituminous raw material in a first pyrolysis reactor to produce a first pyrolysis gas and a first inorganic byproduct; Separating the raw material into a liquid product, pyrolyzing the bituminous raw material pyrolyzed in the first pyrolysis reactor in a second pyrolysis reactor installed at the lower end of the first pyrolysis reactor to produce a second pyrolysis gas and a second inorganic byproduct, Separating the second pyrolysis gas into a second gaseous product and a second liquid product in a second gas-liquid separator, and separating the first liquid product and the second liquid product into bitumen collected in the first collecting tank and the second collecting tank, A pyrolysis method of the raw material can be provided.

The step of generating the first pyrolysis gas and the first inorganic byproduct may include a step of supplying the raw materials to the first pyrolysis reactor and a step of raising the temperature of the first pyrolysis reactor charged with the raw materials to a first temperature Wherein the first pyrolytic reactor heated to the first temperature gradually increases the temperature from the first temperature to the second temperature to pyrolyze the bituminous raw material.

The step of generating the second pyrolytic gas and the second inorganic byproduct may include a step of introducing the raw materials into the second pyrolytic reactor and a step of introducing the raw materials into the second pyrolytic reactor, The second pyrolysis reactor having been heated to the third temperature may gradually increase the temperature from the third temperature to the fourth temperature to pyrolyze the bituminous raw material.

The step of generating the first pyrolysis gas and the first inorganic byproduct may include a step of raising the temperature of the first pyrolysis reactor to a first temperature and a step of raising the temperature of the first pyrolysis reactor to the first pyrolysis reactor, Wherein the first pyrolytic reactor heated to the first temperature is able to thermally decompose the bituminous raw material while maintaining the first temperature.

The step of generating the second pyrolytic gas and the second inorganic byproduct may include a step of raising the temperature of the second pyrolytic reactor to a second temperature higher than the first temperature, The second pyrolytic reactor heated to the second temperature may pyrolyze the bituminous raw material while the second temperature is maintained.

The method may further include burning at least one of the first gaseous product and the second gaseous product in the combustion unit.

The method may further include the step of exchanging heat between any one of the first inorganic byproduct and the second inorganic byproduct and the first and second gaseous products in the heat exchanger.

The embodiments of the present invention can provide a pyrolysis apparatus and a pyrolysis method of a bituminous raw material capable of continuously recovering oils having different boiling points contained in a raw material for biting.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view of a pyrolysis apparatus for a bituminous raw material according to a first embodiment of the present invention; FIG.
Fig. 2 is a view showing a modification of Fig. 1. Fig.
Fig. 3 is a view showing the combustion section of Fig. 2. Fig.
Fig. 4 is a view showing another modification of Fig. 1. Fig.
5 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.
6 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.
7 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.
FIG. 8 is a graph showing the thermal weight of a bituminous raw material pyrolyzed by a non-isothermal method or an isothermal method.
9 is a graph showing the concentrations of gaseous products generated during the process of pyrolysis of the bituminous raw materials in the non-isothermal or isothermal manner.
10 is a graph showing the mass of the liquid product recovered from the non-isothermal pyrolyzed bituminous feedstock.
11 is a graph showing the mass of the liquid product recovered from the bituminous raw material pyrolyzed by the isothermal method.
12 is a view showing a pyrolysis apparatus for a bituminous raw material according to a second embodiment of the present invention.
13 is a view showing a modification of Fig.
14 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.
15 is a view showing a pyrolysis apparatus for a bituminous raw material according to a third embodiment of the present invention.
16 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of Fig.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, configurations and operations according to embodiments of the present invention will be described in detail with reference to the accompanying drawings. DETAILED DESCRIPTION OF THE INVENTION The following description is one of many aspects of the claimed invention and the following description may form part of the detailed description of the invention.

However, the detailed description of known configurations or functions in describing the present invention may be omitted for clarity.

While the invention is susceptible to various modifications and its various embodiments, it is intended to illustrate the specific embodiments and the detailed description. It is to be understood, however, that the invention is not to be limited to the specific embodiments, but includes all modifications, equivalents, and alternatives falling within the spirit and scope of the invention.

Terms including ordinals such as first, second, etc. may be used to describe various elements, but the elements are not limited by such terms. These terms are used only to distinguish one component from another.

It is to be understood that when an element is referred to as being "connected" or "connected" to another element, it may be directly connected or connected to the other element, .

The terminology used in this application is used only to describe a specific embodiment and is not intended to limit the invention. The singular expressions include plural expressions unless the context clearly dictates otherwise.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view of a pyrolysis apparatus for a bituminous raw material according to a first embodiment of the present invention; FIG.

An apparatus 10 for pyrolyzing a bituminous raw material according to an embodiment of the present invention is a device for continuously producing a gas product (methane gas) and a liquid product (oil) by pyrolyzing a bituminous raw material in multi- A first gas-liquid separator 300, a second pyrolysis reactor 400, a second gas-liquid separator 500, a first collecting tank 600, a second collecting tank 700, (800).

In this embodiment, the bituminous raw material may be used to mean a bituminous containing mineral which is contained in large quantities of recoverable oils through pyrolysis.

Such a bituminous raw material may be stored in the storage tank 100 and the bituminous raw material stored in the storage tank 100 may be selectively supplied to the first pyrolysis reactor 200 as needed.

Although not shown, a heating jacket may be mounted on the outer surface of the storage tank 100 because the bituminous raw material has a high viscosity. This is for easy transfer of the bituminous raw material, so that the viscosity of the bituminous raw material can be lowered by applying heat to the bituminous raw material by the heating jacket. In addition, a first screw feeder (not shown) may be provided between the storage tank 100 and the first pyrolysis reactor 200 to facilitate the transfer of the raw materials.

The first pyrolysis reactor (200) can pyrolyze the bituminous raw material. To this end, the first pyrolysis reactor 200 may be heated to a first temperature. At this time, the first pyrolysis reactor (200) may directly heat the raw materials for biting, and may add pyrolysis raw materials to the raw materials by adding heat sources directly supplied or produced from the outside. The first pyrolysis reactor 200 may be provided with a reactor thermometer (not shown) for measuring the reaction temperature.

On the other hand, since the boiling points of the oils recoverable from the bituminous raw materials are all different, the pyrolysis temperature is a very important factor in the pyrolysis of the bituminous raw material.

Accordingly, when the first pyrolysis reactor 200 is heated to the first temperature, the first pyrolysis reactor 200 gradually increases the temperature from the first temperature to the second temperature to pyrolyze the bituminous raw material. For example, the first pyrolysis reactor (200) may be pyrolyzed with the temperature of about 350 ° C to about 450 ° C to pyrolyze the bituminous raw material. In this process, since all of the oils having boiling points between about 350 DEG C and about 450 DEG C can be recovered, the oil recovery rate can be improved.

Alternatively, the first pyrolysis reactor 200 may pyrolyze the bituminous raw material while maintaining the first temperature.

On the other hand, the bituminous raw material pyrolyzed in the first pyrolysis reactor 200 can be separated into the first pyrolysis gas and the first inorganic byproduct. This pyrolysis process is an oxygen-free process, and the pyrolysis gas may mainly be a volatile substance of C, H, and O series. In one example, the first inorganic byproduct may be calcium carbonate (CaCO ₃ ).

The first pyrolysis gas separated in the first pyrolysis reactor (200) may be supplied to the first gas-liquid separator (300). For this purpose, a first pyrolysis gas flow meter (not shown) and a first pyrolysis gas control valve (not shown) for controlling the flow rate of the first pyrolysis gas may be provided at the front end of the first gas-liquid separator 300.

The first gas-liquid separator 300 can separate the first gas product and the first liquid product by cooling the first pyrolysis gas. In one embodiment the first gas product is methane (CH ₄₎ may be a gas, a first liquid product can be oil. The first liquid product may be collected in the first collecting tank 600.

Meanwhile, as described above, when the first pyrolysis reactor 200 is gradually heated from the first temperature to the second temperature to pyrolyze the bituminous raw material, characteristics of the first liquid product recovered according to the pyrolysis temperature are different And the first collecting tank 600 may be provided in plural.

On the other hand, the bituminous raw material that is pyrolyzed in the first pyrolysis reactor 200 and from which the first gaseous product and the first liquid product are recovered may be supplied to the second pyrolysis reactor 400 and pyrolyzed again.

For this purpose, the second pyrolysis reactor (400) may be installed at the lower end of the first pyrolysis reactor (200). In addition, a second screw feeder (not shown) may be provided between the first pyrolysis reactor 200 and the second pyrolysis reactor 400 to facilitate the transfer of the raw materials.

The second pyrolysis reactor 400 has a function of pyrolyzing the bituminous raw material pyrolyzed in the first pyrolysis reactor 200 to a pyrolysis temperature different from that of the first pyrolysis reactor 200. The pyrolysis of the first pyrolysis reactor 200, Temperature to a third temperature higher than the second temperature.

At this time, the second pyrolysis reactor (400) may gradually increase the temperature from the third temperature to the fourth temperature to pyrolyze the bituminous raw material. For example, the first pyrolysis reactor 200 may be pyrolyzed at a temperature of about 450 ° C to about 550 ° C to pyrolyze the bituminous raw material. In this process, oils having boiling points between about 450 ° C and about 550 ° C can be continuously recovered.

Alternatively, the second pyrolysis reactor 400 may pyrolyze the bituminous raw material while maintaining the second temperature higher than the first temperature.

Meanwhile, the bituminous raw material pyrolyzed in the second pyrolysis reactor (400) may generate the second pyrolysis gas and the second inorganic byproduct, and the second pyrolysis gas may be supplied to the second gas-liquid separator (500).

For this purpose, a second pyrolysis gas flow meter (not shown) and a second pyrolysis gas control valve (not shown) for controlling the flow rate of the second pyrolysis gas may be provided at the front end of the second gas-liquid separator 500.

The second gas-liquid separator 500 can separate the second gas product and the second liquid product by cooling the second pyrolysis gas. And the second liquid product can be collected in the second collecting tank 700.

Meanwhile, as described above, when the second pyrolytic reactor 400 is gradually heated from the third temperature to the fourth temperature to pyrolyze the bituminous raw material, the characteristics of the second liquid product recovered according to the pyrolysis temperature are different, The second collection tank 700 may be provided in plural.

Meanwhile, the controller 800 may control the operation of the first pyrolysis reactor 200, the first gas-liquid separator 300, the second pyrolysis reactor 400, and the second gas-liquid separator 500.

Specifically, the controller 800 receives the measured or analyzed values from the reactor thermometer, the first pyrolysis gas flow meter, and the second pyrolysis gas flow meter, and receives the measured values from the first pyrolysis gas control valve, The operation of the pyrolysis gas control valve, the operation of the first and second pyrolysis reactors 200 and 400, and the operation of the first and second gas-liquid separators 300 and 500. For example, the control unit 800 may be a small built-in computer, and may include a data processing unit including a program, a memory, and a CPU.

The program may control the opening amount of the first pyrolysis gas control valve and the second pyrolysis gas control valve based on the values measured or analyzed from the reactor thermometer, the first pyrolysis gas flow meter, and the second pyrolysis gas flow meter, The operation of the first and second pyrolysis reactors 200 and 400, and the operation of the first and second gas-liquid separators 300 and 500. The program may be stored in a memory unit such as a computer storage medium, such as a flexible disk, a compact disk, a hard disk, or an MO (magneto optical disk), and installed in the control unit 800.

Hereinafter, a modification of the pyrolysis apparatus for a bituminous raw material according to an embodiment of the present invention will be described with reference to FIGS. 2 and 3. FIG.

Fig. 2 is a view showing a modification of Fig. 1, and Fig. 3 is a view showing a combustion section of Fig.

2 and 3, the thermal decomposition apparatus 11 includes a storage tank 100, a first thermal decomposition reactor 200, a first gas-liquid separator 300, a second thermal decomposition reactor 400, a second gas-liquid separator 500 A first collecting tank 600, a second collecting tank 700, a control unit 800, and a combustion unit 900.

The pyrolysis apparatus 11 disclosed in FIGS. 2 and 3 is the same as the pyrolysis apparatus 10 described with reference to FIG. 1 except for the combustion section 900. Hereinafter, the combustion section 900 The description of the same embodiment and the reference numerals will be omitted for the same parts.

Combustion unit 900 may provide the heat source needed to pyrolyze the bituminous feedstock. For this purpose, the combustion section 900 may include a combustor 910, a heater 920 and an air supplier 930.

The combustor 910 may receive at least one of the first gaseous product and the second gaseous product.

Specifically, a first gaseous product flow meter (not shown) that measures the flow rate of the first gaseous product flowing into the combustor 910 and a first gaseous product control valve (not shown) that controls the flow rate of the first gaseous product A second gaseous product flow meter (not shown) that measures the flow rate of the second gaseous product of the second gaseous product flowing into the combustor 910, or the first gaseous product flow meter (not shown) The second gas product can be introduced into the combustor 910 via a second gas product control valve (not shown) that controls the flow rate of the second gas product.

In addition, the combustor 910 can receive air through the air supplier 930. Then, when at least one of the first gaseous product and the second gaseous product is heated to a temperature equal to or higher than the firing point by the heater 920, at least one of the first gaseous product and the second gaseous product is combusted in the combustor 910 .

At this time, the controller 800 controls the amount of heat generated by the heater 920 and the amount of opening of the first and second gas product control valves to control the degree of combustion of the first and second gas products.

The generated heat is supplied to at least one of the first pyrolysis reactor 200 and the second pyrolysis reactor 400 by preheating the bituminous fuel stored in the storage tank 100, And can be used as a heat source necessary for pyrolysis of the raw materials for bitumen.

In addition, during combustion of at least one of the first gas product and the second gas product in the combustor 910, exhaust gas such as carbon dioxide (CO ₂ ) may be generated. At this time, the exhaust gas is discharged to an exhaust gas outlet (not shown) provided in the combustor 910, and then supplied to at least one of the first pyrolysis reactor 200 and the second pyrolysis reactor 400, It can be used as a necessary heat source.

As described above, the thermal cracking apparatus 11 according to an embodiment of the present invention burns at least one of the first gaseous product and the second gaseous product generated during the pyrolysis of the bituminous raw material, As a heat source, it is possible to maximize the energy efficiency required for pyrolysis of the bituminous raw material and to reduce the running cost.

Hereinafter, another modification of the pyrolysis apparatus for a bituminous raw material according to an embodiment of the present invention will be described with reference to FIG.

Fig. 4 is a view showing another modification of Fig. 1. Fig.

4, the thermal decomposition apparatus 12 includes a storage tank 100, a first thermal decomposition reactor 200, a first gas-liquid separator 300, a second thermal decomposition reactor 400, a second gas-liquid separator 500, 1 collecting tank 600, a second collecting tank 700, a control unit 800, and a heat exchanger 1000.

4, except for the heat exchanger 1000, is the same as the pyrolyzer 10 described with reference to FIG. 1, so that the heat exchanger 1000 corresponding to the difference will be referred to as a center And the description of the above-mentioned embodiment and the reference numerals will be used for the same parts.

The heat exchanger 1000 may provide the heat source needed to pyrolyze the bituminous feedstock. For this purpose, the heat exchanger 1000 may be supplied with at least one of the first inorganic byproduct and the second inorganic byproduct.

A first gaseous product measuring device (not shown) for measuring the flow rate of the first gaseous product flowing into the heat exchanger 1000 and a first gaseous product control valve (not shown) for controlling the flow rate of the first gaseous product (Not shown) for measuring the flow rate of the first gaseous product flowing into the heat exchanger 1000 or the second gaseous product flowing into the heat exchanger 1000 and the second gaseous product stream The second gaseous product can be introduced into heat exchanger 1000 via a second gaseous product control valve (not shown). At this time, the amount of opening of the first and second gas product control valves may be controlled by the controller 800. [

Accordingly, at least one of the first inorganic byproduct and the second inorganic byproduct may be heat-exchanged with at least one of the first gaseous product and the second gaseous product.

At least one of the first gaseous product and the second gaseous product exchanged with at least one of the first inorganic byproduct and the second inorganic byproduct in the heat exchanger 1000 may be introduced into the storage tank 100 or may be introduced into the first pyrolysis reactor May be introduced into at least one of the first pyrolysis reactor (200) and the second pyrolysis reactor (400).

In this case, when at least one of the first gaseous product and the second gaseous product exchanged with the at least one of the first inorganic byproduct and the second inorganic byproduct in the heat exchanger 1000 flows into the storage tank 100, At least one of the gaseous product and the second gaseous product may heat the bituminous raw material stored in the storage tank 100. In this case, the thermal decomposition efficiency of the first thermal cracking reactor 200 can be improved by supplying the bituminous raw material to the first thermal cracking reactor 200 in a state preheated to some extent.

At least one of the first gaseous product and the second gaseous product exchanged with at least one of the first inorganic byproduct and the second inorganic byproduct in the heat exchanger 1000 is introduced into the first pyrolysis reactor 200 and the second pyrolysis reactor At least one of the heated first gaseous product and the second gaseous product is introduced into at least one of the first pyrolysis reactor (200) and the second pyrolysis reactor (400) . Accordingly, energy required for operation of at least one of the first pyrolysis reactor (200) and the second pyrolysis reactor (400) can be reduced.

Hereinafter, an example of a pyrolysis method for a bituminous raw material according to an embodiment of the present invention will be described with reference to FIG. 5 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.

Referring to FIG. 5, in the first pyrolysis reactor 200, the raw materials for the bitumen are pyrolyzed to produce the first pyrolysis gas and the first inorganic byproducts (S100).

In this case, in the first pyrolysis reactor 200, the raw materials for the bitumen can be pyrolyzed in a non-isothermal or isothermal manner. In this embodiment, the non-isothermal method may mean raising the temperature of the bituminous raw material while changing the temperature, and the isothermal method means raising the temperature of the bituminous raw material to a constant temperature.

First, when the raw bitumen material is pyrolyzed in the non-isothermal manner in the first pyrolysis reactor 200, the raw materials for the raw materials for biting are supplied to the first pyrolysis reactor 200. Then, when the raw materials for the bitumen are fed into the first pyrolysis reactor 200, the temperature of the first pyrolysis reactor 200 is raised to the first temperature.

Next, the first pyrolytic reactor 200, which has been heated to the first temperature, is gradually heated from the first temperature to the second temperature to pyrolyze the bituminous raw material. Thus, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal method, first, the first pyrolysis reactor 200 is heated to a first temperature. Thereafter, when the temperature of the first pyrolysis reactor (200) is raised to the first temperature, the raw materials for the raw materials of the first pyrolysis reactor (200) are supplied.

The first pyrolysis reactor (200), which has been heated to the first temperature, pyrolyzes the raw materials of the bitumen while maintaining the first temperature. Thus, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Meanwhile, the first pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the first gas-liquid separator 300 and separated into the first gas product and the first liquid product (S200).

Next, the bituminous raw material pyrolyzed in the first pyrolysis reactor 200 is pyrolyzed again by the second pyrolysis reactor 400 to produce a second pyrolysis gas and a second inorganic by-product (S300).

As in the first pyrolysis reactor 200, the raw materials for the bitumen in the second pyrolysis reactor 400 may be pyrolyzed in a non-isothermal or isothermal manner.

First, when the bitumen raw material is pyrolyzed in a non-isothermal manner in the second pyrolysis reactor 300, when a raw material for biting is input to the second pyrolysis reactor 400 and a raw material for biting is input to the second pyrolysis reactor 400, The pyrolysis reactor 400 is heated to a third temperature higher than the second temperature.

Then, the second pyrolysis reactor (400), which has been heated to the third temperature, is gradually heated from the third temperature to the fourth temperature to pyrolyze the bituminous raw material. Accordingly, the second pyrolysis gas and the second inorganic by-product are produced in the second pyrolysis reactor (400).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal manner, the second pyrolysis reactor 400 is heated to a second temperature higher than the first temperature, and when the second pyrolysis reactor 400 is heated to the second temperature, The raw materials for the bitumen are fed into the pyrolysis reactor (400).

Next, the second pyrolysis reactor (400), which has been heated to the second temperature, pyrolyzes the raw materials of the bitumen while maintaining the second temperature. As a result, the second pyrolysis gas is generated in the second pyrolysis reactor (400).

Meanwhile, the second pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the second gas-liquid separator 500 to be separated into the second gas product and the second liquid product (S400).

Then, the first liquid product and the second liquid product are collected in the first collecting tank 600 and the second collecting tank 700, respectively (S500).

Hereinafter, a modification of the method for pyrolyzing a bituminous raw material according to an embodiment of the present invention will be described with reference to FIG. 6 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.

Referring to FIG. 6, first the pyrolysis raw material is pyrolyzed in the first pyrolysis reactor 200 to produce a first pyrolysis gas and a first inorganic byproduct (S100).

In this case, in the first pyrolysis reactor 200, the raw materials for the bitumen can be pyrolyzed in a non-isothermal or isothermal manner. In the present embodiment, the non-isothermal method means raising the temperature of the bituminous raw material while changing the temperature, and the isothermal method means raising the temperature of the bituminous raw material to a constant temperature.

First, when the raw bitumen material is pyrolyzed in the non-isothermal manner in the first pyrolysis reactor 200, the raw materials for the raw materials for biting are supplied to the first pyrolysis reactor 200. Then, when the raw materials for the bitumen are fed into the first pyrolysis reactor 200, the temperature of the first pyrolysis reactor 200 is raised to the first temperature.

Next, the first pyrolytic reactor 200, which has been heated to the first temperature, is gradually heated from the first temperature to the second temperature to pyrolyze the bituminous raw material. As a result, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal method, first, the first pyrolysis reactor 200 is heated to a first temperature. Thereafter, when the temperature of the first pyrolysis reactor (200) is raised to the first temperature, the raw materials for the raw materials of the first pyrolysis reactor (200) are supplied.

The first pyrolysis reactor (200), which has been heated to the first temperature, pyrolyzes the raw materials of the bitumen while maintaining the first temperature. As a result, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Meanwhile, the first pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the first gas-liquid separator 300 and separated into the first gas product and the first liquid product (S200).

Next, the bituminous raw material pyrolyzed in the first pyrolysis reactor 200 is pyrolyzed again by the second pyrolysis reactor 400 to produce a second pyrolysis gas and a second inorganic by-product (S300).

As in the first pyrolysis reactor 200, the raw materials for the bitumen in the second pyrolysis reactor 400 may be pyrolyzed in a non-isothermal or isothermal manner.

First, when the bitumen raw material is pyrolyzed in a non-isothermal manner in the second pyrolysis reactor 300, when a raw material for biting is input to the second pyrolysis reactor 400 and a raw material for biting is input to the second pyrolysis reactor 400, The pyrolysis reactor 400 is heated to a third temperature higher than the second temperature.

Then, the second pyrolysis reactor (400), which has been heated to the third temperature, is gradually heated from the third temperature to the fourth temperature to pyrolyze the bituminous raw material. Accordingly, the second pyrolysis gas and the second inorganic byproduct are produced in the second pyrolysis reactor (400).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal manner, the second pyrolysis reactor 400 is heated to a second temperature higher than the first temperature, and when the second pyrolysis reactor 400 is heated to the second temperature, The raw materials for the bitumen are fed into the pyrolysis reactor (400).

Next, the second pyrolysis reactor (400), which has been heated to the second temperature, pyrolyzes the raw materials of the bitumen while maintaining the second temperature. As a result, the second pyrolysis gas and the second inorganic byproduct are produced in the second pyrolysis reactor (400).

Meanwhile, the second pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the second gas-liquid separator 500 to be separated into the second gas product and the second liquid product (S400).

Then, the first liquid product and the second liquid product are collected in the first collecting tank 600 and the second collecting tank 700, respectively (S500).

Finally, at least one of the first gas product and the second gas product is burned in the combustion unit 900 (S600). Thus, a heat source necessary for pyrolysis of the bituminous raw material can be provided.

Hereinafter, another modification of the method for pyrolyzing a bituminous raw material according to an embodiment of the present invention will be described with reference to FIG. 7 is a flowchart showing a method of pyrolysis using the pyrolysis apparatus of FIG.

Referring to FIG. 7, first the pyrolysis raw material is pyrolyzed in the first pyrolysis reactor 200 to produce a first pyrolysis gas and a first inorganic byproduct (S100).

In this case, in the first pyrolysis reactor 200, the raw materials for the bitumen can be pyrolyzed in a non-isothermal or isothermal manner. In the present embodiment, the non-isothermal method means raising the temperature of the bituminous raw material while changing the temperature, and the isothermal method means raising the temperature of the bituminous raw material to a constant temperature.

First, when the raw bitumen material is pyrolyzed in the non-isothermal manner in the first pyrolysis reactor 200, the raw materials for the raw materials for biting are supplied to the first pyrolysis reactor 200. Then, when the raw materials for the bitumen are fed into the first pyrolysis reactor 200, the temperature of the first pyrolysis reactor 200 is raised to the first temperature.

Next, the first pyrolytic reactor 200, which has been heated to the first temperature, is gradually heated from the first temperature to the second temperature to pyrolyze the bituminous raw material. As a result, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal method, first, the first pyrolysis reactor 200 is heated to a first temperature. Thereafter, when the temperature of the first pyrolysis reactor (200) is raised to the first temperature, the raw materials for the raw materials of the first pyrolysis reactor (200) are supplied.

The first pyrolysis reactor (200), which has been heated to the first temperature, pyrolyzes the raw materials of the bitumen while maintaining the first temperature. As a result, the first pyrolysis gas and the first inorganic byproduct are produced in the first pyrolysis reactor (200).

Meanwhile, the first pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the first gas-liquid separator 300 and separated into the first gas product and the first liquid product (S200).

Next, the bituminous raw material pyrolyzed in the first pyrolysis reactor 200 is pyrolyzed again by the second pyrolysis reactor 400 to produce a second pyrolysis gas and a second inorganic by-product (S300).

As in the first pyrolysis reactor 200, the raw materials for the bitumen in the second pyrolysis reactor 400 may be pyrolyzed in a non-isothermal or isothermal manner.

First, when the bitumen raw material is pyrolyzed in a non-isothermal manner in the second pyrolysis reactor 300, when a raw material for biting is input to the second pyrolysis reactor 400 and a raw material for biting is input to the second pyrolysis reactor 400, The pyrolysis reactor 400 is heated to a third temperature higher than the second temperature.

Then, the second pyrolysis reactor (400), which has been heated to the third temperature, is gradually heated from the third temperature to the fourth temperature to pyrolyze the bituminous raw material. Accordingly, the second pyrolysis gas and the second inorganic byproduct are produced in the second pyrolysis reactor (400).

Alternatively, when the bituminous raw material is pyrolyzed in an isothermal manner, the second pyrolysis reactor 400 is heated to a second temperature higher than the first temperature, and when the second pyrolysis reactor 400 is heated to the second temperature, The raw materials for the bitumen are fed into the pyrolysis reactor (400).

Next, the second pyrolysis reactor (400), which has been heated to the second temperature, pyrolyzes the raw materials of the bitumen while maintaining the second temperature. As a result, the second pyrolysis gas and the second inorganic byproduct are produced in the second pyrolysis reactor (400).

Meanwhile, the second pyrolysis gas generated by pyrolysis by the non-isothermal method or the isothermal method is supplied to the second gas-liquid separator 500 to be separated into the second gas product and the second liquid product (S400).

Then, the first liquid product and the second liquid product are collected in the first collecting tank 600 and the second collecting tank 700, respectively (S500).

Finally, in the heat exchanger 1000, any one of the first inorganic byproduct and the second inorganic by-product is exchanged with one of the first gas product and the second gas product (S700). Accordingly, at least one of the first gaseous product and the second gaseous product heated through the heat exchanger 1000 can be utilized as a heat source necessary for pyrolysis of the raw materials for the bitumen.

Hereinafter, the results of the pyrolysis of the bituminous raw material using the pyrolysis apparatus according to this embodiment will be described with reference to FIGS. 8 to 11. FIG.

FIG. 8 is a graph showing the thermal weight of the bituminous raw material pyrolyzed by the non-isothermal method or the isothermal method, and FIG. 9 is a graph showing the concentration of the gaseous product generated during the pyrolysis of the raw materials of the bituminous raw material or the isothermal method .

8 and 9, the applicant of the present invention has found that at a temperature of 10 ° C / min to set the pyrolysis temperature range in which the bituminous raw materials can be most efficiently pyrolyzed in the first pyrolysis reactor 200 and the second pyrolysis reactor 400, min, the change in the weight of the bituminous raw material was measured while the bituminous raw material was heated.

As a result, it was found that the thermal weight of the bituminous raw material was steadily reduced as the bituminous raw material was heated. This shows that when the bituminous raw material is pyrolyzed, the volatile component (i.e., oil) is recovered from the bituminous raw material.

Specifically, it can be seen that the thermal weight loss is greatest in the range of about 350 ° C to about 550 ° C. Thus, the pyrolysis zone is divided into a first zone (about 0 ° C. to about 350 ° C.), a second zone (about 350 ° C. to about 450 ° C.), and a third zone (about 450 ° C. to about 550 ° C.) Pyrolysis.

As a result, light oil having a boiling point of about 0 ° C to about 350 ° C was recovered in the first section, and heavy oil (boiling oil having a boiling point of about 350 ° C to about 450 ° C in the second section) middle oil) was recovered. In the third section, heavy oil having a boiling point of about 450 ° C to about 550 ° C was recovered.

In addition, when the bituminous raw material is pyrolyzed at a temperature of about 350 ° C to about 550 ° C, the concentration of gaseous products generated from the bituminous raw material is the highest. Thus, it can be seen that when the bituminous raw material is pyrolyzed at a temperature of about 350 ° C. to about 550 ° C., a high concentration of gaseous product is generated from the bituminous raw material, thereby pyrolyzing the bituminous raw material more efficiently.

On the other hand, FIG. 10 is a graph showing the mass of the liquid product recovered from the bituminous raw material pyrolyzed in a non-isothermal manner, and FIG. 11 is a graph showing the mass of the liquid product recovered from the raw material pyrolyzed by the isothermal method.

Referring to FIGS. 10 and 11, the inventors of the present invention have repeatedly conducted experiments and researches on a method for increasing the temperature of a bituminous raw material in order to pyrolyze a bituminous raw material, (Hereinafter referred to as " oil ").

First, a nitrogen (N ₂ ) atmosphere was prepared and the temperature was gradually increased from room temperature to about 550 ° C to pyrolyze the bituminous raw material. Then, the oil was recovered from the pyrolyzed bituminous raw material, and then the mass of the recovered oil was measured using a mass spectrometer.

Further, a nitrogen (N ₂ ) atmosphere was formed, and the bituminous raw material was pyrolyzed while maintaining the temperature at about 550 ° C, and the oil was recovered from the pyrolyzed raw material. Then, the mass of the recovered oil was measured using a mass spectrometer.

As a result, it can be confirmed that the distribution of the mass value of the recovered oil in the bituminous raw material is changed by the method of raising the bituminous raw material to pyrolyze the bituminous raw material.

As a result, it is possible to recover oils having different masses (i.e., oils having different flammability) by selectively applying a method of raising the bituminous raw material to pyrolyze the raw materials of the bituminous materials as needed, .

Hereinafter, a pyrolysis apparatus for a bituminous raw material according to a second embodiment of the present invention and a pyrolysis method using the pyrolysis apparatus will be described with reference to FIG. 12 to FIG. FIG. 12 is a view showing a pyrolysis apparatus for a bituminous raw material according to a second embodiment of the present invention, FIG. 13 is a view showing a modification of FIG. 12, and FIG. 14 is a view for explaining a pyrolysis apparatus Fig.

12 to 14, a pyrolysis apparatus and a pyrolysis apparatus according to the second embodiment are provided with a pyrolysis reactor, a gas-liquid separator and a collecting tank as a single unit, and the heat exchanger is provided with a gas- This is mainly due to the fact that it is connected to the reactor.

Specifically, the pyrolysis apparatus 20 for a bituminous raw material according to the present embodiment is a device for pyrolyzing a bituminous raw material to produce a gaseous product (methane gas) and a liquid product (oil), and includes a storage tank 100, a pyrolysis reactor 200, a gas-liquid separator 300, a collecting tank 600, a control unit 800, and a heat exchanger 1000.

The pyrolysis reactor 200 can pyrolyze the bituminous raw material. For this purpose, the pyrolysis reactor 200 is supplied with the bituminous raw material through the bituminous raw material feed line 150, and the bituminous raw material can be pyrolyzed by raising the bituminous raw material to the first temperature (about 350 ° C). At this time, the heat required for the pyrolysis reactor 200 to be heated to the first temperature (about 350 ° C) can be supplied from the gas product heated in the heat exchanger 1000, which will be described later. This will be described later.

However, the spirit of the present invention is not limited thereto. For example, when the pyrolysis reactor 200 is heated to the first temperature (about 350 ° C.), the pyrolysis reactor 200 gradually increases from the first temperature (about 350 ° C.) to the second temperature (about 550 ° C.) The bituminous raw material may also be pyrolyzed.

At this time, the temperature of the pyrolysis reactor 200 can be controlled by the controller 800.

Specifically, the control unit 800 can control the temperature of the pyrolysis reactor 200 so that the pyrolysis reactor 200 heated to a first temperature (about 350 ° C) maintains a first temperature during a pyrolysis process of the raw materials.

The control unit 800 controls the temperature of the pyrolysis reactor 200 heated to the first temperature (about 350 ° C) to increase from the first temperature (about 350 ° C) to the second temperature (about 550 ° C) So that the temperature of the pyrolysis reactor 200 can be controlled.

On the other hand, the bituminous raw material pyrolyzed in the pyrolysis reactor 200 can be separated into pyrolysis gas and inorganic byproducts. This pyrolysis process is a process that does not require oxygen, and the pyrolysis gas may be mainly C, H, O volatile substances, and the inorganic byproduct may be calcium carbonate (CaCO ₃ ).

The gas-liquid separator 300 can receive the pyrolysis gas and separate it into a gaseous product and a liquid product. To this end, the gas-liquid separator 300 can condense the oil component contained in the pyrolysis gas by supplying the pyrolysis gas through the pyrolysis gas transfer line 250 and cooling the pyrolysis gas. Thereby, the liquid product and the gaseous product can be separated, and the liquid product can be collected in the collection tank 600 through the liquid product transfer line 350, and the gaseous product can be collected in the first gaseous product transfer line 370, To the heat exchanger (1000). In one embodiment the gaseous product may be a methane (CH ₄₎ gas, a liquid product can be oil.

The heat exchanger 1000 may provide the heat source needed to pyrolyze the bituminous feedstock. For this purpose, the heat exchanger 1000 is supplied with inorganic byproducts through the inorganic byproduct transport line 270 and can receive gaseous products through the first gas product transport line 370. The gaseous products can then be heat-exchanged with the inorganic byproducts and heated. At this time, the heat exchanger 1000 is controlled by the controller 800 so that the heated gaseous products can be introduced into the storage tank 100 and the pyrolysis reactor 200 through the second gaseous product transfer line 450 .

At this time, when the heated gaseous product flows into the storage tank 100, the heated gaseous product can heat the bituminous raw material stored in the storage tank 100. In this case, since the bituminous raw material is supplied to the pyrolysis reactor 200 in a preheated state to some extent, the pyrolysis efficiency of the pyrolysis reactor 200 can be increased. Furthermore, since the operation load control of the pyrolysis reactor 200 is facilitated, the operation performance of the pyrolysis apparatus 20 can be enhanced.

In addition, when the heated gaseous product flows into the pyrolysis reactor 200, the heated gaseous product can be used as a pyrolysis heat source in the pyrolysis reactor 200. Accordingly, the energy required for the operation of the pyrolysis reactor 200 can be reduced.

13, the pyrolysis apparatus 21 for a bituminous raw material is connected to the gas-liquid separator 300 and the pyrolysis reactor 200, and a heat source necessary for thermally decomposing the raw materials of the bituminous A combustion section 900 for supplying the combustion gas may be additionally provided.

A method of pyrolyzing a bituminous raw material using the pyrolysis apparatus according to the present embodiment having the above-described structure will now be described.

First, a raw material for bituminous materials is supplied to the pyrolysis reactor 200 (S110).

Then, in the pyrolysis reactor 200, the raw material of the bituminous material is pyrolyzed (S210). In this case, the pyrolysis reactor 200 can be pyrolyzed by an isothermal method. In this embodiment, the isothermal method means raising the temperature of the bituminous raw material to a constant temperature.

Specifically, the pyrolysis reactor 200 is heated to a first temperature. Then, when the pyrolysis reactor 200 is heated to the first temperature, the raw materials for the raw materials for biting are supplied to the pyrolysis reactor 200.

The pyrolysis reactor 200, which has been heated to the first temperature, pyrolyzes the raw materials of the bitumen in a state where the first temperature is maintained by the controller 800.

However, the spirit of the present invention is not limited thereto, and the pyrolysis reactor 200 may be pyrolyzed in a non-isothermal manner. In the present embodiment, the non-isothermal method means raising the temperature of the bituminous raw material while changing the temperature.

Specifically, the raw materials for the bitumen are charged into the pyrolysis reactor (200). Then, when the raw material for bituminous flux is supplied to the pyrolysis reactor 200, the pyrolysis reactor 200 is heated to the first temperature.

Next, the pyrolysis reactor 200, which has been heated to the first temperature, is gradually heated from the first temperature to the second temperature by the control unit 800 to pyrolyze the bituminous raw material.

Thus, the bituminous raw materials pyrolyzed in the isothermal or nonisothermal manner are separated into pyrolysis gas and inorganic byproducts in the pyrolysis reactor (200). At this time, the pyrolysis gas is supplied to the gas-liquid separator 300, and the inorganic by-products are supplied to the heat exchanger 1000.

Meanwhile, the pyrolysis gas pyrolyzed in the pyrolysis reactor 200 is separated into a gaseous product and a liquid product in the gas-liquid separator 300 (S310). Here, the liquid product is stored in the collection tank 600, and the gaseous product is supplied to the heat exchanger 1000 and the combustion unit 700.

The gaseous product separated in the gas-liquid separator 300 and the inorganic by-products pyrolyzed in the pyrolysis reactor 200 are heat-exchanged in the heat exchanger 1000 (S410).

Finally, the gaseous product whose temperature is increased through the heat exchanger 1000 is supplied to at least one of the storage tank 100 and the pyrolysis reactor 200 (S510). Accordingly, the bituminous fuel stored in the storage tank 100 may be heated or a heat source necessary for thermal decomposition of the bituminous raw material may be provided to the thermal decomposition reactor 200.

In addition, the gaseous products supplied to the combustion unit 700 are burned in the combustion unit 700, so that a heat source necessary for pyrolysis of the raw materials of the bituminous material can be provided to the pyrolysis reactor 200.

Hereinafter, a pyrolysis apparatus for a bituminous raw material and a pyrolysis method using the same according to a third embodiment of the present invention will be described with reference to FIGS. 15 and 16. FIG. FIG. 15 is a view showing a pyrolysis apparatus for a bituminous raw material according to a third embodiment of the present invention, and FIG. 16 is a flowchart showing a pyrolysis method using the pyrolysis apparatus of FIG.

15 and 16, the pyrolysis apparatus and the pyrolysis apparatus according to the third embodiment are characterized in that the heat exchanger is replaced with a combustor as compared with the second embodiment described above.

Specifically, the pyrolysis apparatus 30 for a bituminous raw material according to the present embodiment is an apparatus for pyrolyzing a bituminous raw material to produce a gaseous product (methane gas) and a liquid product (oil). The apparatus includes a storage tank 100, a pyrolysis reactor 200, a gas-liquid separator 300, a collecting tank 600, a control unit 800, and a combustion unit 900.

In this embodiment, the bituminous raw material may be used to mean a bituminous containing mineral which is contained in large quantities of recoverable oils through pyrolysis.

The storage tank 100 may store a bituminous raw material. In addition, the bituminous raw material stored in the storage tank 100 may be selectively supplied to the pyrolysis reactor 200 as needed.

Although not shown, a heating jacket may be mounted on the outer surface of the storage tank 100 because the bituminous raw material has a high viscosity. This is for easy transfer of the bituminous raw material, so that the viscosity of the bituminous raw material can be lowered by applying heat to the bituminous raw material by the heating jacket.

The pyrolysis reactor 200 can pyrolyze the bituminous raw material. For this purpose, the pyrolysis reactor 200 is supplied with the bituminous raw material through the bituminous raw material feed line 150, and the bituminous raw material can be pyrolyzed by raising the bituminous raw material to the first temperature (about 350 ° C).

However, the spirit of the present invention is not limited thereto. For example, when the pyrolysis reactor 200 is heated to the first temperature (about 350 ° C.), the pyrolysis reactor 200 gradually increases from the first temperature (about 350 ° C.) to the second temperature (about 550 ° C.) The bituminous raw material may also be pyrolyzed.

At this time, the temperature of the pyrolysis reactor 200 can be controlled by the controller 800.

Specifically, the control unit 800 can control the temperature of the pyrolysis reactor 200 so that the pyrolysis reactor 200 heated to a first temperature (about 350 ° C) maintains a first temperature during a pyrolysis process of the raw materials.

The control unit 800 controls the temperature of the pyrolysis reactor 200 heated to the first temperature (about 350 ° C) to increase from the first temperature (about 350 ° C) to the second temperature (about 550 ° C) So that the temperature of the pyrolysis reactor 200 can be controlled.

On the other hand, the bituminous raw material pyrolyzed in the pyrolysis reactor 200 can be separated into pyrolysis gas and inorganic byproducts. This pyrolysis process is a process that does not require oxygen, and the pyrolysis gas may be mainly C, H, O volatile substances, and the inorganic byproduct may be calcium carbonate (CaCO ₃ ).

The gas-liquid separator 300 can receive the pyrolysis gas and separate it into a gaseous product and a liquid product. To this end, the gas-liquid separator 300 can condense the oil component contained in the pyrolysis gas by supplying the pyrolysis gas through the pyrolysis gas transfer line 250 and cooling the pyrolysis gas. Thereby, the gaseous product and the liquid product can be separated, and the liquid product thereof can be collected in the collection tank 600 through the liquid product transfer line 350. In addition, the gaseous product may be supplied to the combustion section 1000 through the first gaseous product transfer line 370. In one embodiment the gaseous product may be a methane (CH ₄₎ gas, a liquid product can be oil.

Combustion unit 900 may provide the heat source needed to pyrolyze the bituminous feedstock. For this purpose, the combustion section 900 may include a combustor 910, a heater 920 and an air supplier 930.

The combustor 910 is supplied with the gaseous product through the first gas product transfer line 370 and can receive air through the air supplier 930. Then, when the gas product is heated to a temperature equal to or higher than the ignition point by the heater 920, the gaseous product can be burned in the combustor 910.

In this combustion process, heat is generated, and this heat may be used as a heat source for preheating the bituminous fuel stored in the storage tank 100 or supplied to the thermal decomposition reactor 200 to pyrolyze the bituminous raw material.

Meanwhile, exhaust gas such as carbon dioxide (CO 2) may be generated in the process of burning gaseous products in the combustor 910. At this time, the exhaust gas is discharged to the exhaust gas outlet provided in the combustor 910, and then supplied to the pyrolysis reactor 200, so that it can be used as a heat source necessary for pyrolysis of the raw materials of the bituminous material.

A method of pyrolyzing a bituminous raw material using the pyrolysis apparatus according to the present embodiment having the above-described structure will now be described.

First, a raw material for bituminous materials is supplied to the pyrolysis reactor 200 (S110).

Then, in the pyrolysis reactor 200, the raw material of the bituminous material is pyrolyzed (S210). In this case, the pyrolysis reactor 200 can be pyrolyzed by an isothermal method. In this embodiment, the isothermal method means raising the temperature of the bituminous raw material to a constant temperature.

Specifically, the pyrolysis reactor 200 is heated to a first temperature. Then, when the pyrolysis reactor 200 is heated to the first temperature, the raw materials for the raw materials for biting are supplied to the pyrolysis reactor 200.

The pyrolysis reactor 200, which has been heated to the first temperature, pyrolyzes the raw materials of the bitumen in a state where the first temperature is maintained by the controller 800.

However, the spirit of the present invention is not limited thereto, and the pyrolysis reactor 200 may be pyrolyzed in a non-isothermal manner. In the present embodiment, the non-isothermal method means raising the temperature of the bituminous raw material while changing the temperature.

Specifically, the raw materials for the bitumen are charged into the pyrolysis reactor (200). Then, when the raw material for bituminous flux is supplied to the pyrolysis reactor 200, the pyrolysis reactor 200 is heated to the first temperature.

Next, the pyrolysis reactor 200, which has been heated to the first temperature, is gradually heated from the first temperature to the second temperature by the control unit 800 to pyrolyze the bituminous raw material.

Thus, the bituminous raw materials pyrolyzed in the isothermal or nonisothermal manner are separated into pyrolysis gas and inorganic byproducts in the pyrolysis reactor (200). At this time, the pyrolysis gas is supplied to the gas-liquid separator 300.

Meanwhile, the pyrolysis gas pyrolyzed in the pyrolysis reactor 200 is separated into a gaseous product and a liquid product in the gas-liquid separator 300 (S310). Here, the liquid product is stored in the collection tank 600, and the gaseous product is supplied to the combustion unit 900.

The gas product supplied to the combustion unit 900 is burned in the combustion unit 900 so that a heat source necessary for thermal decomposition of the bituminous raw material is provided to the pyrolysis reactor 200 (S420).

While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, You will understand. For example, a person skilled in the art can change the material, size and the like of each constituent element depending on the application field or can combine or substitute the embodiments in a form not clearly disclosed in the embodiments of the present invention, Of the range. Therefore, it should be understood that the above-described embodiments are to be considered in all respects as illustrative and not restrictive, and that such modified embodiments are included in the technical idea described in the claims of the present invention.

10, 11, 12, 20, 21, 30: pyrolysis device of bituminous raw material
100: Storage tank
200: Pyrolysis reactor (first pyrolysis reactor)
300: gas-liquid separator (first gas-liquid separator)
400: second pyrolysis reactor 500: second gas-liquid separator
600: Collection tank (first collection tank) 700: Second collection tank
800: Control part 900: Combustion part
910: Combustor 920: Heater
930: air feeder 1000: heat exchanger

Claims (31)

A reservoir for storing the bituminous raw material;
A first pyrolysis reactor that receives the bituminous raw material from the storage tank and pyrolyzes the bituminous raw material to produce a first pyrolysis gas and a first inorganic byproduct;
A first gas-liquid separator separating the first pyrolysis gas into a first gas product and a first liquid product;
A second pyrolysis reactor installed at a lower end of the first pyrolysis reactor and generating pyrolysis gas and second inorganic pyrolysis by re-pyrolyzing the pyrolyzed raw material pyrolyzed in the first pyrolysis reactor;
A second gas-liquid separator for separating the second pyrolysis gas into a second gas product and a second liquid product;
A first collecting tank for collecting the first liquid product;
A second collecting tank for collecting the second liquid product; And
And a controller for controlling the first pyrolysis reactor, the first gas-liquid separator, the second pyrolysis reactor, and the second gas-
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
A first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator; And
And a second pyrolysis gas control valve for controlling a flow rate of the second pyrolysis gas flowing into the second gas-liquid separator,
Wherein,
And an opening amount of the first pyrolysis gas control valve and an opening amount of the second pyrolysis gas control valve,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
Wherein,
And controlling the temperature of the first pyrolysis reactor to be raised to a first temperature when the bituminous raw material is input to the first pyrolysis reactor,
Pyrolysis equipment for bitumen raw materials. The method of claim 3,
Wherein,
Wherein the first pyrolytic reactor is gradually heated from the first temperature to the second temperature to pyrolyze the bituminous raw material,
Pyrolysis equipment for bitumen raw materials. 5. The method of claim 4,
Wherein,
The second pyrolysis reactor is controlled to raise the temperature to a third temperature higher than the second temperature,
Pyrolysis equipment for bitumen raw materials. 6. The method of claim 5,
Wherein,
And the second pyrolysis reactor is gradually heated from the third temperature to the fourth temperature to pyrolyze the bituminous raw material,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
Wherein,
Wherein the first pyrolytic reactor is heated to a first temperature and then supplied with the bituminous raw material,
Pyrolysis equipment for bitumen raw materials. 8. The method of claim 7,
Wherein,
Wherein the first pyrolysis reactor is controlled to pyrolyze the bituminous raw material while maintaining the first temperature,
Pyrolysis equipment for bitumen raw materials. 9. The method of claim 8,
Wherein,
The second pyrolysis reactor is controlled to raise the temperature to a second temperature higher than the first temperature,
Pyrolysis equipment for bitumen raw materials. 10. The method of claim 9,
Wherein,
And the second pyrolytic reactor is maintained at the second temperature to pyrolyze the bituminous raw material,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
A first screw feeder provided between the storage tank and the first pyrolysis reactor, for transferring the bituminous raw material stored in the storage tank to the first pyrolysis reactor; And
Further comprising a second screw feeder provided between the first pyrolysis reactor and the second pyrolysis reactor for transferring the bitolysed material pyrolyzed in the first pyrolysis reactor to the second pyrolysis reactor,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
Further comprising a heating jacket installed on an outer surface of the storage tank for lowering the viscosity of the bituminous raw material by applying heat to the bituminous raw material stored in the storage tank,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
Further comprising a combustion section for receiving and combusting at least one of the first gas product and the second gas product,
Wherein the combustion section is controlled by the control section,
Pyrolysis equipment for bitumen raw materials. 14. The method of claim 13,
A first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator; And
And a second pyrolysis gas control valve for controlling a flow rate of the second pyrolysis gas flowing into the second gas-
Pyrolysis equipment for bitumen raw materials. 15. The method of claim 14,
A first gas product control valve for controlling a flow rate of the first gaseous product flowing into the combustion unit; And
Further comprising a second gaseous product control valve for controlling a flow rate of the second gaseous product flowing into the combustion section,
Pyrolysis equipment for bitumen raw materials. 16. The method of claim 15,
Wherein,
Wherein the control unit controls the opening amount of the first pyrolysis gas control valve, the opening amount of the second pyrolysis gas control valve, the opening amount of the first gas product control valve, and the opening amount of the second gas product control valve,
Pyrolysis equipment for bitumen raw materials. 14. The method of claim 13,
The burner
And a combustor for receiving and combusting at least one of the first gaseous product and the second gaseous product.
Pyrolysis equipment for bitumen raw materials. 18. The method of claim 17,
The burner
Further comprising a heater disposed below the combustor for heating at least one of the first gaseous product and the second gaseous product,
Pyrolysis equipment for bitumen raw materials. 19. The method of claim 18,
The burner
Further comprising an air supply connected to the combustor and supplying combustion air to the combustor,
Pyrolysis equipment for bitumen raw materials. 18. The method of claim 17,
Wherein at least one of the first gaseous product and the second gaseous product is combusted in the combustor,
Wherein the exhaust gas is discharged to an exhaust gas outlet of the combustor connected to the first pyrolysis reactor or the second pyrolysis reactor and supplied to the first pyrolysis reactor or the second pyrolysis reactor,
Wherein waste heat of the exhaust gas is used as a heat source necessary for pyrolysis of the bituminous raw material,
Pyrolysis equipment for bitumen raw materials. The method according to claim 1,
Further comprising a heat exchanger for receiving any one of the first inorganic byproduct and the second inorganic byproduct, the first gaseous product and the second gaseous product, and exchanging heat with each other,
Wherein the heat exchanger is controlled by the control unit,
Pyrolysis equipment for bitumen raw materials. 22. The method of claim 21,
A first pyrolysis gas control valve for controlling a flow rate of the first pyrolysis gas flowing into the first gas-liquid separator; And
And a second pyrolysis gas control valve for controlling a flow rate of the second pyrolysis gas flowing into the second gas-
Pyrolysis equipment for bitumen raw materials. 23. The method of claim 22,
A first gaseous product control valve for controlling a flow rate of the first gaseous product flowing into the heat exchanger; And
Further comprising a second gaseous product control valve for controlling a flow rate of said second gaseous product entering said heat exchanger,
Pyrolysis equipment for bitumen raw materials. 24. The method of claim 23,
Wherein,
Wherein the control unit controls the opening amount of the first pyrolysis gas control valve, the opening amount of the second pyrolysis gas control valve, the opening amount of the first gas product control valve, and the opening amount of the second gas product control valve,
Pyrolysis equipment for bitumen raw materials. The first pyrolysis reactor and the first pyrolysis gas are pyrolyzed to produce a first pyrolysis gas and a first inorganic byproduct;
Separating the first pyrolysis gas into a first gaseous product and a first liquid product in a first gas-liquid separator;
The pyrolytic raw material pyrolyzed in the first pyrolytic reactor installed at the lower end of the first pyrolytic reactor is pyrolyzed again to produce a second pyrolytic gas and a second inorganic byproduct;
Separating the second pyrolysis gas into a second gaseous product and a second liquid product in a second gas-liquid separator; And
Wherein the first liquid product and the second liquid product are collected in a first collecting tank and a second collecting tank, respectively,
Method of pyrolysis of bituminous raw materials. 26. The method of claim 25,
Wherein the first pyrolysis gas and the first inorganic byproduct are generated,
Introducing the bituminous raw material into the first pyrolysis reactor; And
And raising the temperature of the first pyrolysis reactor charged with the bituminous raw material to a first temperature,
The first pyrolysis reactor, which has been heated to the first temperature,
And gradually pyrolyzing the bituminous raw material while being gradually heated from the first temperature to the second temperature,
Method of pyrolysis of bituminous raw materials. 27. The method of claim 26,
Wherein the second pyrolysis gas and the second inorganic byproduct are produced,
Introducing the bituminous raw material into the second pyrolysis reactor; And
And raising the temperature of the second pyrolysis reactor charged with the bituminous raw material to a third temperature higher than the second temperature,
The second pyrolytic reactor, which has been heated to the third temperature,
And gradually pyrolyzing the bituminous raw material while being gradually heated from the third temperature to the fourth temperature,
Method of pyrolysis of bituminous raw materials. 26. The method of claim 25,
Wherein the first pyrolysis gas and the first inorganic byproduct are generated,
Raising the temperature of the first pyrolysis reactor to a first temperature; And
And introducing the bituminous raw material into the first pyrolysis reactor heated to the first temperature,
The first pyrolysis reactor, which has been heated to the first temperature,
And pyrolyzing the bituminous raw material while maintaining the first temperature,
Method of pyrolysis of bituminous raw materials. 29. The method of claim 28,
Wherein the second pyrolysis gas and the second inorganic byproduct are produced,
Raising the temperature of the second pyrolysis reactor to a second temperature higher than the first temperature; And
Further comprising the step of injecting the bituminous raw material into the second pyrolysis reactor heated to the second temperature,
The second pyrolytic reactor, which has been heated to the second temperature,
And pyrolyzing the bituminous raw material while maintaining the second temperature,
Method of pyrolysis of bituminous raw materials. 26. The method of claim 25,
Further comprising the step of burning at least one of the first gaseous product and the second gaseous product at the combustion zone,
Method of pyrolysis of bituminous raw materials. 26. The method of claim 25,
Further comprising the step of heat exchange between any one of said first inorganic byproduct and said second inorganic byproduct and either said first gaseous product or said second gaseous product in a heat exchanger,
Method of pyrolysis of bituminous raw materials.

Images